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Número de publicaciónUS20090016938 A1
Tipo de publicaciónSolicitud
Número de solicitudUS 11/776,587
Fecha de publicación15 Ene 2009
Fecha de presentación12 Jul 2007
Fecha de prioridad12 Jul 2007
También publicado comoCN101687168A, CN101687168B, EP2175984A1, EP2175984B1, US7868129, WO2009009038A1
Número de publicación11776587, 776587, US 2009/0016938 A1, US 2009/016938 A1, US 20090016938 A1, US 20090016938A1, US 2009016938 A1, US 2009016938A1, US-A1-20090016938, US-A1-2009016938, US2009/0016938A1, US2009/016938A1, US20090016938 A1, US20090016938A1, US2009016938 A1, US2009016938A1
InventoresLarry Cates Windes, Bruce Roger DeBruin, Michael Paul Ekart
Cesionario originalEastman Chemical Company
Exportar citaBiBTeX, EndNote, RefMan
Enlaces externos: USPTO, Cesión de USPTO, Espacenet
Sloped tubular reactor with spaced sequential trays
US 20090016938 A1
Resumen
A sloped tubular reactor operable to facilitate a chemical reaction in a reaction medium flowing therethrough. The reactor can include a plurality of spaced apart internal trays disposed at different elevations in a downwardly sloping elongated tubular member.
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Reclamaciones(65)
1. A process comprising: subjecting a reaction medium to a chemical reaction in a reactor comprising a downwardly sloped elongated tubular member and a plurality of spaced apart trays disposed in said tubular member, wherein said tubular member is elongated along a central axis of elongation that is oriented at a downward angle in the range of from about 5 to about 75 degrees below horizontal, wherein each of said trays presents an upwardly facing surface across which at least a portion of said reaction medium flows as said reaction medium flows through said reactor.
2. The process of claim 1, wherein said upwardly facing surface is sloped less than about 25 degrees from horizontal.
3. The process of claim 2, wherein said downward angle of said tubular member is in the range of from about 10 to about 60 degrees below horizontal.
4. The process of claim 1, wherein said upwardly facing surface is sloped less than about 5 degrees from horizontal, wherein said downward angle of said tubular member is in the range of from about 12 to about 45 degrees below horizontal.
5. The process of claim 1, wherein said upwardly facing surface is substantially planar and substantially horizontal.
6. The process of claim 1, wherein said reaction medium flows by gravity through said reactor.
7. The process of claim 1, wherein said reactor comprises at least four of said trays located at different elevations in said tubular member.
8. The process of claim 7, wherein said tubular member is a pipe.
9. The process of claim 8, wherein each of said trays is substantially flat and substantially horizontal.
10. The process of claim 1, wherein said tubular member has a length-to-diameter (L:D) ratio in the range of from about 2:1 to about 50:1.
11. The process of claim 10, wherein L is in the range of from about 10 to about 200 feet and D is in the range of from about 1 to about 20 feet.
12. The process of claim 1, wherein at least one of said trays defines a plurality of apertures through which a first portion of said reaction medium pass as said reaction medium flows through said reactor.
13. The process of claim 12, wherein said at least one of said trays presents a terminal edge over which a second portion of said reaction medium passes as said reaction medium flows through said reactor.
14. The process of claim 1, wherein each of said trays presents a coupling edge and a terminal edge, wherein said coupling edge is sealingly coupled to the inside wall of said tubular member, wherein said terminal edge is spaced from the inside wall of said tubular member to thereby provide a flow passageway through which said reaction medium can pass.
15. The process of claim 14, wherein said tubular member is a substantially straight downwardly sloping pipe, wherein each of said trays is substantially flat and substantially horizontal, wherein each of said trays has a generally truncated oval shape with said coupling edge defining the curved portion of the truncated oval and said terminal edge defining the truncated portion of the truncated oval.
16. The process of claim 15, wherein each of said trays defines a plurality of apertures through which at least a portion of said reaction medium flows.
17. The process of claim 16, wherein each of said trays is in the range of from about 5 to about 80 percent open.
18. The process of claim 16, wherein a first portion of said reaction medium flows downwardly through said apertures and a second portion of said reaction medium flows over said terminal edge and downwardly through said flow passageway.
19. The process of claim 16, wherein said reactor comprises in the range of from 2 to 50 of said trays.
20. The process of claim 1, wherein a vapor byproduct of said chemical reaction flows generally upwardly and/or downwardly in said tubular member as said reaction medium flows generally downwardly in said tubular member.
21. The process of claim 20, further comprising withdrawing at least a portion of said vapor byproduct from said reactor via a vapor outlet located near the top and/or bottom of said reactor.
22. The process of claim 1, further comprising introducing a feed into said reactor at a feed inlet located near the top of said reactor, further comprising withdrawing a predominately liquid product from said reactor at a product outlet located near the bottom of said reactor.
23. The process of claim 1, wherein said chemical reaction comprises polycondensation, wherein the average chain length of said reaction medium increases by at least about 10 in said reactor.
24. The process of claim 23, further comprising introducing a polycondensation feed into a feed inlet of said reactor, wherein said polycondensation feed forms said reaction medium in said reactor, wherein said polycondensation feed has an average chain length in the range of from about 5 to about 50.
25. The process of claim 24, wherein said polycondensation feed is maintained at a temperature in the range of from about 220 to about 350° C., wherein the vapor space pressure in said reactor is maintained in the range of from about 0 to about 30 torr.
26. The process of claim 23, wherein said reaction medium comprises a polyester polymer or copolymer that is at least partly formed by said polycondensation.
27. The process of claim 26, wherein said polyester polymer or copolymer comprises polyethylene terephthalate (PET).
28. The process of claim 1, wherein PET is produced by said reactor.
29. The process of claim 28, wherein said PET is a PET copolymer comprising at least about 90 mole percent ethylene terephthalate repeat units and up to 10 percent of added comonomer repeat units.
30. The process of claim 29, wherein said added comonomer repeat units are derived from an added comonomer selected from the group consisting of isophthalic acid, 2,6-naphthaline-dicarboxylic acid, 1,4-cyclohexanedimethanol, diethylene glycol, and combinations of two or more thereof.
31. The process of claim 30, wherein said added comonomer comprises isophthalic acid.
32. The process of claim 28, wherein said PET is produced by said reactor at a rate of at least about 10,000 pounds per hour.
33. The process of claim 1, wherein said chemical reaction comprises polycondensation, wherein the average chain length of said reaction medium increases by at least about 2 in said reactor.
34. The process of claim 33, further comprising introducing a feed into a feed inlet of said reactor, wherein said feed forms said reaction medium in said reactor, wherein said feed has an average chain length in the range of from about 1 to about 20.
35. The process of claim 34, wherein said feed is maintained at a temperature in the range of from about 220 to about 350° C., wherein the vapor space pressure in said reactor is maintained in the range of from about 0 to about 300 torr.
36. The process of claim 1, wherein said reactor comprises no mechanical mixing device.
37. A process for making polyethylene terephthalate (PET), said process comprising:
(a) introducing a polycondensation feed into a polycondensation reactor, wherein said polycondensation feed forms a predominately liquid reaction medium in said reactor, wherein said polycondensation feed comprises PET having an average chain length in the range of from about 5 to about 50;
(b) subjecting said reaction medium to polycondensation in said reactor, wherein said reactor comprises a substantially straight downwardly sloped pipe and at least four spaced apart trays disposed at different elevations in said pipe, wherein said pipe is sloped downwardly at an angle in the range of from about 10 to about 60 degrees below horizontal, wherein said reaction medium flows primarily by gravity through said reactor, wherein each of said trays presents an upwardly facing surface across which at least a portion of said reaction medium flows as said reaction medium flows through said reactor, wherein said upwardly facing surface is sloped less than about 10 degrees from horizontal, wherein each of said trays defines a plurality of apertures through which at least a portion of said reaction medium passes as said reaction medium flows through said reactor; and
(c) recovering a predominately liquid polycondensation product from said reactor, wherein said polycondensation product comprises PET having an average chain length that is at least about 10 greater than the average chain length of the PET in said polycondensation feed.
38. The process of claim 37, wherein said upwardly facing surface is substantially planar and substantially horizontal.
39. The process of claim 37, wherein each of said trays defines a terminal edge over which at least a portion of said reaction medium passes as said reaction medium flows through said reactor.
40. The process of claim 39, wherein each of said trays is substantially flat and substantially horizontal, wherein each of said trays presents a coupling edge sealingly coupled to the inside wall of said pipe, wherein said terminal edge is spaced from the inside wall of said pipe to thereby provide a flow passageway between said terminal edge and the inside wall of said pipe, wherein at least a portion of said reaction medium flows downwardly through said flow passageway after passing over said terminal edge.
41. The process of claim 40, wherein said polycondensation causes the formation of a vapor byproduct in said reactor, wherein at least a portion of said vapor byproduct flows generally upwardly and/or downwardly through said flow passageway as said at least a portion of said reaction medium flows downwardly through said flow passageway.
42. The process of claim 40, wherein each of said trays has a generally truncated oval shape with said coupling edge defining the curved portion of the truncated oval and the terminal edge defining the truncated portion of the truncated oval.
43. The process of claim 37, wherein said polycondensation feed is introduced into said reactor via a feed inlet located near the top of said reactor, wherein a vapor byproduct of said polycondensation is discharged from said reactor via a vapor outlet located near the top and/or bottom of said reactor, wherein said polycondensation product is recovered from a product outlet located near the bottom of said reactor.
44. The process of claim 37, wherein said polycondensation feed comprises PET having an average chain length in the range of from about 8 to about 40, wherein said polycondensation product comprises PET having an average chain length that is at least about 25 greater than the average chain length of the PET in said polycondensation feed.
45. The process of claim 37, wherein the temperature of said reaction medium in said reactor is maintained in the range of from about 220 to about 350° C., wherein the pressure of said reaction medium in said reactor is maintained in the range of from about 0 to about 30 torr.
46. A reactor comprising: a downwardly sloped tubular member and a plurality of spaced apart trays disposed at different elevations in said tubular member, wherein said tubular member is elongated along a central axis of elongation that is oriented at a downward angle in the range of from about 5 to about 75 degrees below horizontal, wherein each of said trays presents an upwardly facing surface, wherein said upwardly facing surface is sloped less than about 25 degrees from horizontal.
47. The reactor of claim 46, wherein at least one of said trays defines a plurality of apertures extending downwardly therethrough.
48. The reactor of claim 46, wherein at least one of said trays defines a terminal edge that is spaced from the inside wall of said tubular member.
49. The reactor of claim 46, wherein said reactor comprises at least four of said trays.
50. The reactor of claim 46, wherein said tubular member comprises a substantially straight pipe.
51. The reactor of claim 46, wherein said upwardly facing surface is sloped less than about 5 degrees from horizontal, wherein said downward angle of said tubular member is in the range of from about 10 to about 60 degrees below horizontal.
52. The reactor of claim 46, wherein said upwardly facing surface is substantially planar and substantially horizontal.
53. The reactor of claim 46, wherein said tubular member has a length-to-diameter (L:D) ratio in the range of from about 2:1 to about 50:1.
54. The reactor of claim 53, wherein L is in the range of from about 10 to about 200 feet and D is in the range of from about 1 to about 20 feet.
55. The reactor of claim 46, wherein said tubular member is a substantially straight downwardly sloping pipe, wherein each of said trays is substantially flat and substantially horizontal.
56. The reactor of claim 55, wherein each of said trays presents a coupling edge and a terminal edge, wherein said coupling edge is sealingly coupled to the inside wall of said pipe, wherein said terminal edge is spaced from the inside wall of said pipe to thereby define a flow passageway between said terminal edge and the inside wall of said pipe.
57. The reactor of claim 56, wherein each of said trays has a generally truncated oval shape with said coupling edge defining the curved portion of the truncated oval and said terminal edge defining the truncated portion of the truncated oval.
58. The reactor of claim 53, wherein each of said trays defines a plurality of apertures extending downwardly therethrough.
59. The reactor of claim 58, wherein said reactor comprises at least four of said trays.
60. The reactor of claim 46, wherein said reactor defines a feed inlet located near the top of said reactor, a vapor outlet located near the top of said reactor, and a product outlet located near the bottom of said reactor.
61. The process of claim 1, further comprising introducing a feed into a feed inlet of said reactor, wherein said feed forms said reaction medium in said reactor, wherein said feed has an It.V. in the range of from 0.1 to 0.5 dL/g.
62. The process of claim 1, further comprising removing a product from a product outlet of said reactor, wherein said reaction medium forms said product in said reactor, wherein the It.V. of said product is in the range of from about 0.3 to about 1.2 dL/g.
63. The process of claim 24 further comprising removing a polycondensation product from a product outlet of said reactor, wherein said reaction medium forms said polycondensation product, wherein the It.V. of said polycondensation product is in the range of from about 0.3 to about 1.2 dL/g.
64. The process of claim 37 wherein the It.V. of said polycondensation feed is in the range of from 0.1 and 0.5 dL/g.
65. The process of claim 37 wherein the It.V. of said polycondensation product is in the range of from 0.3 to 1.2 dL/g.
Descripción
    BACKGROUND OF THE INVENTION
  • [0001]
    1. Field of the Invention
  • [0002]
    This invention relates to reactors for processing liquid-containing reaction mediums. In another aspect, the invention concerns polycondensation reactors used for melt-phase production of polyesters.
  • [0003]
    2. Description of the Prior Art
  • [0004]
    Melt-phase polymerization can be used to produce a variety of polyesters, such as, for example, polyethylene terephthalate (PET). PET is widely used in beverage, food, and other containers, as well as in synthetic fibers and resins. Advances in process technology coupled with increased demand have led to an increasingly competitive market for the production and sale of PET. Therefore, a low-cost, high-efficiency process for producing PET is desirable.
  • [0005]
    Generally, melt-phase polyester production facilities, including those used to make PET, employ an esterification stage and a polycondensation stage. In the esterification stage, polymer raw materials (i.e., reactants) are converted to polyester monomers and/or oligomers. In the polycondensation stage, polyester monomers exiting the esterification stage are converted into a polymer product having the desired final average chain length.
  • [0006]
    In many conventional melt-phase polyester production facilities, esterification and polycondensation are carried out in one or more mechanically agitated reactors, such as, for example, continuous stirred tank reactors (CSTRs). However, CSTRs and other mechanically agitated reactors have a number of drawbacks that can result in increased capital, operating, and/or maintenance costs for the overall polyester production facility. For example, the mechanical agitators and various control equipment typically associated with CSTRs are complex, expensive, and can require extensive maintenance.
  • [0007]
    Thus, a need exists for a high efficiency polyester process that minimizes capital, operating, and maintenance costs while maintaining or enhancing product quality.
  • SUMMARY OF THE INVENTION
  • [0008]
    In one embodiment of the present invention, there is provided a process comprising subjecting a reaction medium to a chemical reaction in a reactor comprising a downwardly sloped elongated tubular member and a plurality of spaced apart trays disposed in the tubular member. The tubular member is elongated along a central axis of elongation that is oriented at a downward angle in the range of from about 5 to about 75 degrees below horizontal. Each of the trays presents an upwardly facing surface across which at least a portion of the reaction medium flows as the reaction medium flows through the reactor.
  • [0009]
    In another embodiment of the present invention, there is provided a process for making polyethylene terephthalate (PET), the process comprising: (a) introducing a polycondensation feed into a polycondensation reactor, wherein the polycondensation feed forms a predominately liquid reaction medium in the reactor, wherein the polycondensation feed comprises PET having an average chain length in the range of from about 5 to about 100; (b) subjecting the reaction medium to polycondensation in the reactor, wherein the reactor comprises a substantially straight downwardly sloped pipe and at least four spaced apart trays disposed at different elevations in the pipe, wherein the pipe is sloped downwardly at an angle in the range of from about 10 to about 60 degrees below horizontal, wherein the reaction medium flows primarily by gravity through the reactor, wherein each of the trays presents an upwardly facing surface across which at least a portion of the reaction medium flows as the reaction medium flows through the reactor, wherein the upwardly facing surface is sloped less than about 10 degrees from horizontal, wherein each of the trays defines a plurality of apertures through which at least a portion of the reaction medium passes as the reaction medium flows through the reactor; and (c) recovering a predominately liquid polycondensation product from the reactor, wherein the polycondensation product comprises PET having an average chain length that is at least about 10 greater than the average chain length of the PET in the polycondensation feed.
  • [0010]
    In still another embodiment of the present invention, there is provided a reactor comprising a downwardly sloped tubular member and a plurality of spaced apart trays disposed at different elevations in the tubular member. The tubular member is elongated along a central axis of elongation that is oriented at a downward angle in the range of from about 5 to about 75 degrees below horizontal. Each of the trays presents an upwardly facing surface that is sloped less than about 25 degrees from horizontal.
  • BRIEF DESCRIPTION OF THE DRAWINGS
  • [0011]
    Certain embodiments of the present invention are described in detail below with reference to the enclosed figures, wherein:
  • [0012]
    FIG. 1 is a cut-away top view a sloped tubular reactor configured in accordance with one embodiment of the present invention and suitable for use as a polycondensation reactor in a melt-phase polyester production facility; and
  • [0013]
    FIG. 2 is a partial sectional side view of the sloped tubular reactor taken along line 2-2 in FIG. 1, particularly illustrating the manner in which a reaction medium passes over and through the series of spaced apart internal trays as it progresses downwardly through the reactor.
  • DETAILED DESCRIPTION
  • [0014]
    FIGS. 1 and 2 illustrate an exemplary sloped tubular reactor configured in accordance with one embodiment of the present invention. The configuration and operation of the reactor depicted in FIGS. 1 and 2 are described in detail below. Although certain portions of the following description relate primarily to reactors employed in a melt-phase polyester production process, reactors configured in accordance with embodiments of the present invention may find application in a wide variety of chemical processes. For example, reactors configured in accordance with certain embodiments of the present invention may be advantageously employed in any process where chemical reactions take place in the liquid phase of a reaction medium and a vapor is produced as a result of the chemical reaction. Further, reactors configured in accordance with certain embodiments of the present invention may be advantageously employed in chemical processes that are enhanced by increasing the surface area of the reaction medium.
  • [0015]
    Referring now to FIGS. 1 and 2, one embodiment of a sloped tubular reactor 10 is illustrated as generally comprising a vessel shell 12 and a series of spaced apart internal trays 14 a-e disposed in shell 12. Vessel shell 12 comprises a downwardly sloping tubular member 16, an upper end cap 18 coupled to the top of tubular member 16, and a lower end cap 20 coupled to the bottom of tubular member 16. Vessel shell 12 defines a feed inlet 22 near the top of reactor 10, a liquid product outlet 24 near the bottom of reactor 10, and a vapor outlet 26 near the top of reactor 10.
  • [0016]
    Tubular member 16 is elongated along a downwardly sloping central axis of elongation. In certain embodiments of the present invention, the central axis of elongation of tubular member 16 is sloped at an angle in the range of from about 5 to about 75 degrees below horizontal, about 10 to about 60 degrees below horizontal, or 12 to 45 degrees below horizontal. In the embodiment illustrated in FIGS. 1 and 2, tubular member 16 is a substantially straight, substantially cylindrical, elongated pipe. However, in certain embodiments, tubular member 16 can be an elongated tubular member having a variety of cross-sectional configurations (e.g., rectangular, square, or oval).
  • [0017]
    Vessel shell 12 and/or tubular member 16 can have a maximum internal length (L) that is greater than its maximum internal diameter (D). In certain embodiments, shell 12 and/or tubular member 16 has a length-to-diameter (L:D) ratio in the range of from about 2:1 to about 50:1, about 4:1 to about 30:1, or 8:1 to 20:1. In certain embodiments, L is in the range of from about 10 to about 200 feet, about 20 to about 150 feet, or 30 to 80 feet, and D is in the range of from about 1 to about 20 feet, about 2 to about 10 feet, or 3 to 5 feet.
  • [0018]
    Internal trays 14 a-e present respective upwardly facing surfaces 28 a-e across which a liquid can flow, as described in detail below. In the embodiment illustrated in FIGS. 1 and 2, upwardly facing surfaces 28 a-e of trays 14 a-e are substantially planar and substantially horizontal. Alternatively, upwardly facing surfaces can extend at any angle that is within about 25 degrees of horizontal, within about 10 degrees of horizontal, or within 3 degrees of horizontal.
  • [0019]
    Trays 14 a-e each define a plurality of downwardly extending apertures 30 a-e through which a liquid can flow. Alternatively, at least one or a majority of trays can define a plurality of downwardly extending apertures through which a liquid can flow. The number, size, and shape of apertures 30 a-e can vary greatly depending, for example, on the production capacity of reactor 10 and the viscosity of the medium processed therein. In certain embodiments of the present invention, each tray 14 a-e defines in the range of from about 5 to about 200,000 apertures, about 200 to about 50000 apertures, or 1000 to 10000 apertures. In certain embodiments of the present invention, the average number of holes per unit area is in the range from about 0.5 to about 50 holes per square inch, about 1 to about 20 holes per square inch, or 3 to 10 holes per square inch. In certain embodiments of the present invention, the percent open of each tray 14 a-e is in the range of from about 5 to about 80 percent, about 10 to about 60 percent, or 15 to 50 percent.
  • [0020]
    Trays 14 a-e each present respective terminal edges 32 a-e that are spaced from the inside wall of tubular member 16. Alternatively, at least one or a majority of trays can present terminal edges that are spaced from the inside wall of tubular member 16. Flow passageways 34 a-e are defined by the gaps between the inside wall of tubular member 16 and terminal edges 32 a-e of trays 14 a-e, respectively. One or more of trays 14 a-e can, optionally, be equipped with an upwardly extending weir located proximate terminal edges 32 a-e. Trays 14 a-e also present respective coupling edges 36 a-e that are sealingly coupled to the inside wall of tubular member 16 by any suitable method (e.g., welding).
  • [0021]
    In the embodiment illustrated in FIGS. 1 and 2, each tray 14 a-e is a substantially flat, substantially horizontal plate that is sealingly coupled to the inside wall of downwardly sloped tubular member 16 at its respective coupling edge 36 a-e. Thus, in the embodiment depicted in FIGS. 1 and 2, the shape of each tray 14 a-e can generally be that of a truncated oval, with coupling edges 36 a-e defining the curved portion of the oval and terminal edges 32 a-e defining the truncated portion of the oval.
  • [0022]
    Although FIGS. 1 and 2, show trays 14 a-e as being supported in tubular member 16 via the rigid attachment of coupling edges 36 a-e to the inside wall of tubular member 16, it should be noted that a variety of mechanisms for supporting trays 14 a-e in tubular member 16 can be employed. For example, trays 14 a-e can be supported in tubular members 16 using support members that support trays 14 a-e from the bottom of tubular member 16 and/or suspend trays 14 a-e from the top of tubular member 16. However, if the sides of trays 14 a-e are spaced from the inside wall of tubular member, tray sidewalls may be required to keep reaction medium from prematurely flowing around the sides of trays 14 a-e.
  • [0023]
    In the embodiment illustrated in FIGS. 1 and 2, each tray 14 a-e has a substantially identical configuration. However, in certain embodiments of the present invention, the orientation and/or configuration of trays 14 a-e can be different in order to optimize the configuration of reactor 10 to match the application for with reactor 10 is employed. For example, when reactor 10 is used to process a reaction medium whose viscosity increases as it flows downwardly through reactor 10, it may be desirable for trays 14 a-e to have an increasing downward slope to facilitate the flow of the higher viscosity reaction medium across the lower trays. Further, in such an application, it may be desired for the size of apertures 30 a-e, number of apertures 30 a-e, or percent open of trays 14 a-e to increase downwardly to facilitate flow of the higher viscosity reaction medium through the lower trays.
  • [0024]
    The total number of internal trays 14 employed in reactor 10 can vary greatly depending on a variety of factors such as, for example, the length of tubular member 16, the slope of tubular member 16, and the viscosity of the medium processed in reactor 10. In certain embodiments of the present invention, the number of trays 14 employed in reactor 10 can be at least 4, at least 6, or in the range of from about 2 to about 50, about 4 to about 25, or 6 to 15.
  • [0025]
    In operation, a predominately liquid feed is introduced into reactor 10 via feed inlet 22. In the upper portion of reactor 10, the feed forms a predominately liquid reaction medium 38 that flows downwardly on the bottom of tubular member 16 until it reaches uppermost internal tray 14 a.
  • [0026]
    Once reaction medium 38 is on uppermost tray 14 a, it flows across the upwardly facing surface 28 a. When tray 14 a is configured with apertures 30 a, a portion of reaction medium 38 passes downwardly through apertures 30 a and onto the bottom of tubular member 16 and/or onto the upwardly facing surface 28 b of the next lower tray 14 b. In accordance with one embodiment of the present invention, the portion of reaction medium 38 that passes through apertures 30 a forms strands that extend below tray 14 a. These strands can greatly increase the surface area of reaction medium 38 when compared to the flow of reaction medium 38 through a non-trayed tubular member or across a tray without apertures. In one embodiment, reaction medium 38 flows primarily by gravity through reactor 10.
  • [0027]
    The portion of reaction medium 38 that does not pass through apertures 30 a flows over terminal edge 32 a of tray 14 a, passes downwardly through flow passageway 34 a, and onto the next lower tray 14 b. When tray 14 a is equipped with a weir, the portion of the reaction medium flowing over terminal edge 32 a must pass over, around, through openings in, and/or under the weir prior to entering flow passageway 34 a. Flow of reaction medium 38 over and through the remaining trays 14 b-e can occur in generally the same manner as described above for uppermost tray 14 a.
  • [0028]
    As reaction medium 38 flows through reactor 10, a chemical reaction takes place within reaction medium 38. A vapor 40 can be formed in reactor 10. Vapor 40 can comprise one or more byproducts of the chemical reaction carried out in reactor 10 and/or one or more volatile compounds present in the feed to reactor 10 that vaporize therein. Vapor 40 is disengaged from and flows generally upwardly and over reaction medium 38 as reaction medium 38 progresses downwardly through reactor 10. In particular, vapor 40 generated in the lower portion of reactor 10 can pass upwardly through flow passageways 34 a-e countercurrent to reaction medium 38 passing downwardly through flow passageways 34 a-e. Vapor 40 exits reactor 10 via vapor outlet 26, while reaction medium 38 exits reactor 10 as a predominately liquid product via liquid product outlet 24. Alternatively, vapor 40 can flow generally downwardly with reaction medium 38 and exit a vapor outlet (not shown) located near the lower end of reactor 10.
  • [0029]
    As mentioned above, weirs can be employed on one or more trays 14 a-e to help maintain the desired depth of reaction medium 38 on trays 14 a-e. In one embodiment of the present invention, the maximum depth of reaction medium 38 on each tray 14 a-e is less than about 0.8D, less than about 0.4D, or less than 0.25D, where D is the maximum internal diameter of tubular member 16.
  • [0030]
    Sloped tubular reactors configured in accordance with certain embodiments of the present invention require little or no mechanical agitation of the reaction medium processed therein. Although the reaction medium processed in the sloped tubular reactor may be somewhat agitated by virtue of flowing through the reactor and falling from one reactor level to another, this flow agitation and gravitational agitation is not mechanical agitation. In one embodiment of the present invention, less than about 50 percent, less than about 25 percent, less than about 10 percent, less than about 5 percent, or 0 percent of the total agitation of the reaction medium processed in the sloped tubular reactor is provided by mechanical agitation. Thus, reactors configured in accordance with certain embodiments of the present invention can operate without any mechanical mixing devices. This is in direct contrast to conventional continuous stirred tank reactors (CSTRs) which employ mechanical agitation almost exclusively.
  • [0031]
    As indicated above, sloped tubular reactors configured in accordance with embodiments of the present invention reactors can be used in a variety of chemical processes. In one embodiment, a sloped tubular reactor configured in accordance with the present invention is employed in a melt-phase polyester production facility capable of producing any of a variety of polyesters from a variety of starting materials. Examples of melt-phase polyesters that can be produced in accordance with embodiments of the present invention include, but are not limited to, polyethylene terephthalate (PET), which includes homopolymers and copolymers of PET; fully aromatic or liquid crystalline polyesters; biodegradable polyesters, such as those comprising butanediol, terephthalic acid and adipic acid residues; poly(cyclohexane-dimethylene terephthalate) homopolymer and copolymers; and homopolymers and copolymers of 1,4-cyclohexane-dimethanol (CHDM) and cyclohexane dicarboxylic acid or dimethyl cyclohexanedicarboxylate. When a PET copolymer is produced, such copolymer can comprise at least 90, at least 91, at least 92, at least 93, at least 94, at least 95, at least 96, at least 97, at least 98 mole percent of ethylene terephthalate repeat units and up to 10, up to 9, up to 8, up to 7, up to 6, up to 5, up to 4, up to 3, or up to 2 mole percent of added comonomer repeat units. Generally, the comonomer repeat units can be derived from one or more comonomers selected from the group consisting of isophthalic acid, 2,6-naphthaline-dicarboxylic acid, CHDM, and diethylene glycol.
  • [0032]
    In general, a polyester production process according to certain embodiments of the present invention can comprise two main stages—an esterification stage and a polycondensation stage. In the esterification stage, the polyester starting materials, which can comprise at least one alcohol and at least one acid, are subjected to esterification to thereby produce polyester monomers and/or oligomers. In the polycondensation stage, the polyester monomers and/or oligomers from the esterification stage are reacted into the final polyester product. As used herein with respect to PET, monomers have less than 3 chain lengths, oligomers have from about 7 to about 50 chain lengths (components with a chain length of 4 to 6 units can be considered monomer or oligomer), and polymers have greater than about 50 chain lengths. A dimer, for example, EG-TA-EG-TA-EG, has a chain length of 2, and a trimer 3, and so on.
  • [0033]
    The acid starting material employed in the esterification stage can be a dicarboxylic acid such that the final polyester product comprises at least one dicarboxylic acid residue having in the range of from about 4 to about 15 or from 8 to 12 carbon atoms. Examples of dicarboxylic acids suitable for use in the present invention can include, but are not limited to, terephthalic acid, phthalic acid, isophthalic acid, naphthalene-2,6-dicarboxylic acid, cyclohexanedicarboxylic acid, cyclohexanediacetic acid, diphenyl-4,4′-dicarboxylic acid, diphenyl-3,4′-dicarboxylic acid, 2,2,-dimethyl-1,3-propandiol, dicarboxylic acid, succinic acid, glutaric acid, adipic acid, azelaic acid, sebacic acid, and mixtures thereof. In one embodiment, the acid starting material can be a corresponding ester, such as dimethyl terephthalate instead of terephthalic acid.
  • [0034]
    The alcohol starting material employed in the esterification stage can be a diol such that the final polyester product can comprise at least one diol residue, such as, for example, those originating from cycloaliphatic diols having in the range of from about 3 to about 25 carbon atoms or 6 to 20 carbon atoms. Suitable diols can include, but are not limited to, ethylene glycol (EG), diethylene glycol, triethylene glycol, 1,4-cyclohexane-dimethanol, propane-1,3-diol, butane-1,4-diol, pentane-1,5-diol, hexane-1,6-diol, neopentylglycol, 3-methylpentanediol-(2,4), 2-methylpentanediol-(1,4), 2,2,4-trimethylpentane-diol-(1,3), 2-ethylhexanediol-(1,3), 2,2-diethylpropane-diol-(1,3), hexanediol-(1,3), 1,4-di-(hydroxyethoxy)-benzene, 2,2-bis-(4-hydroxycyclohexyl)-propane, 2,4-dihydroxy-1,1,3,3-tetramethyl-cyclobutane, 2,2,4,4tetramethyl-cyclobutanediol, 2,2-bis-(3-hydroxyethoxyphenyl)-propane, 2,2-bis-(4-hydroxy-propoxyphenyl)-propane, isosorbide, hydroquinone, BDS-(2,2-(sulfonylbis)4,1-phenyleneoxy))bis(ethanol), and mixtures thereof.
  • [0035]
    In addition, the starting materials can comprise one or more comonomers. Suitable comonomers can include, for example, comonomers comprising terephthalic acid, dimethyl terephthalate, isophthalic acid, dimethyl isophthalate, dimethyl-2,6-naphthalenedicarboxylate, 2,6-naphthalene-dicarboxylic acid, ethylene glycol, diethylene glycol, 1,4-cyclohexane-dimethanol (CHDM), 1,4-butanediol, polytetramethyleneglyocl, trans-DMCD, trimellitic anhydride, dimethyl cyclohexane-1,4dicarboxylate, dimethyl decalin-2,6dicarboxylate, decalin dimethanol, decahydronaphthalane 2,6-dicarboxylate, 2,6-dihydroxymethyl-decahydronaphthalene, hydroquinone, hydroxybenzoic acid, and mixtures thereof.
  • [0036]
    According to one embodiment of the present invention, the esterification in the esterification stage can be carried out at a reaction medium temperature in the range of from about 180 to about 350° C., or about 215 to about 305° C., or 260 to 290° C. and a vapor space pressure of less than about 70 psig, in the range of from about −4 to about 10 psig, or 2 to 5 psig. The average chain length of the monomer and/or oligomer exiting the esterification stage can be in the range of from about 1 to about 20, about 2 to about 15, or 5 to 12.
  • [0037]
    Reactors configured in accordance with certain embodiments of the present invention can be employed in a melt-phase polyester production system as a prepolymer reactor for carrying out a prepolymerization step and/or as a finisher reactor for carrying out a finishing step. A detailed description of the process conditions for the present invention employed as a prepolymer reactor and/or a finisher reactor is given below with reference to FIG. 1. It is understood that reactors configured in accordance with embodiments of the present invention can generally be employed as prepolymer reactors and/or finisher reactors and that these process conditions are not limited to the embodiment described in FIG. 1.
  • [0038]
    Referring again to FIG. 1, when reactor 10 is employed as a prepolymer reactor in a melt-phase polyester production process (e.g., a process for making PET), more than one chemical reaction can be carried out in reactor 10. For example, although polycondensation may be the predominate chemical reaction carried out in reactor 10, a certain amount of esterification may also occur in reactor 10. When reactor 10 is employed as a prepolymer reactor, the average chain length of the feed introduced into feed inlet 22 can be in the range of from about 1 to about 20, about 2 to about 15, or 5 to 12, while the average chain length of the predominately liquid product withdrawn from liquid product outlet 24 can be in the range of from about 5 to about 50, about 8 to about 40, or 10 to 30. When reactor 10 is employed as a prepolymerization reactor, the chemical reaction carried out in reactor 10 can cause the average chain length of reaction medium 38 to increase by at least about 2, in the range of from about 5 to about 30, or in the range of from 8 to 20 between feed inlet 22 and liquid product outlet 24.
  • [0039]
    When reactor 10 is employed as a prepolymer reactor, the feed can enter feed inlet 22 at a temperature in the range of from about 220 to about 350° C., about 265 to about 305° C., or 270 to 290° C. The predominately liquid product exiting liquid product outlet 24 can have a temperature within about 50° C., 25° C., or 10° C. of the temperature of the feed entering feed inlet 22. In one embodiment, the temperature of the liquid product exiting liquid product outlet 24 is in the range of from about 220 to about 350° C., about 265 to about 305° C., or 270 to 290° C. In one embodiment, the average temperature of reaction medium 38 in reactor 10 is in the range of from about 220 to about 350° C., about 265 to about 305° C., or 270 to 290° C. The average temperature of reaction medium 38 is the average of at least three temperature measurements taken at equal spacings along the primary flow path of reaction medium 38 through reactor 10, where the temperature measurements are each taken near the cross sectional centroid of reaction medium 38 (as opposed to near the wall of the reactor or near the upper liquid surface of the reaction medium). When reactor 10 is employed as a prepolymer reactor, the vapor space pressure in reactor 10 (measured at vapor outlet 26) can be maintained in the range of from about 0 to about 300 torr, in the range of from about 1 to about 50 torr, or in the range of from 20 to 30 torr.
  • [0040]
    When reactor 10 is employed as a prepolymer reactor, it may be desirable to heat the feed prior to introduction into reactor 10 and/or it may be desirable to heat reaction medium 38 as it flows through reactor 10. Generally, the cumulative amount of heat added to the feed immediately upstream of reactor 10 plus any heat added to reaction medium 38 in reactor 10 can be in the range of from about 100 to about 5,000 BTU/lb, in the range of from about 400 to about 2,000 BTU/lb, or in the range of from 600 to 1,500 BTU/lb.
  • [0041]
    Referring again to FIG. 1, when reactor 10 is employed as a finisher reactor in a melt-phase polyester production process (e.g., a process for making PET), the average chain length of the feed introduced into feed inlet 22 can be in the range of from about 5 to about 50, about 8 to about 40, or 10 to 30, while the average chain length of the predominately liquid product withdrawn from liquid product outlet 24 can be in the range of from about 30 to about 210, about 40 to about 80, or 50 to 70. Generally, the polycondensation carried out in reactor 10 can cause the average chain length of reaction medium 38 to increase by at least about 10, at least about 25, or at least 50 between feed inlet 22 and liquid product outlet 24.
  • [0042]
    When reactor 10 is employed as a finisher reactor, the feed can enter feed inlet 22 at a temperature in the range of from about 220 to about 350° C., about 265 to about 305° C., or 270 to 290° C. The predominately liquid product exiting liquid product outlet 24 can have a temperature within about 50° C., 25° C., or 10° C. of the temperature of the feed entering feed inlet 22. In one embodiment, the temperature of the liquid product exiting liquid product outlet 24 is in the range of from about 220 to about 350° C., about 265 to about 305° C., or 270 to 290° C. In one embodiment, the average temperature of reaction medium 38 in reactor 10 is in the range of from about 220 to about 350° C., about 265 to about 305° C., or 270 to 290° C. When reactor 10 is employed as a finisher reactor, the vapor space pressure in reactor 10 (measured at vapor outlet 26) can be maintained in the range of from about 0 to about 30 torr, in the range of from about 1 to about 20 torr, or in the range of from 2 to 10 torr.
  • [0043]
    Reactors configured in accordance with embodiments of the present invention can provide numerous advantages when employed as reactors in the polycondensation stages of a polyester production process. Such reactors can be particularly advantageous when employed as prepolymer and/or finisher reactors in a process for making PET. Further, such reactors are well suited for use in commercial scale PET production facilities capable of producing PET at a rate of at least about 10,000 pounds per hours, at least about 100,000 pounds per hour, at least about 250,000 pounds per hour, or at least 500,000 pounds per hour.
  • [0044]
    In one embodiment of the present invention, there is provided a process comprising subjecting a reaction medium to a chemical reaction in a reactor comprising a downwardly sloped elongated tubular member and a plurality of spaced apart trays disposed in the tubular member. The tubular member is elongated along a central axis of elongation that is oriented at a downward angle in the range of from about 5 to about 75 degrees below horizontal. Each of the trays presents an upwardly facing surface across which at least a portion of the reaction medium flows as the reaction medium flows through the reactor. The detailed description of FIGS. 1 and 2, such as the tubular member, trays, and reaction medium flow, apply to this embodiment.
  • [0045]
    In one example, a product is removed from a product outlet of the reactor, wherein the reaction medium forms the product in the reactor. Additionally, when the chemical reaction comprises polycondensation, the product can be a polycondensation product. The It.V. of the product or polycondensation product can be in the range of from about 0.3 to about 1.2, about 0.35 to about 0.6, or 0.4 to 0.5 dL/g. In one example, It.V. of the product or polycondensation product is in the range of from about 0.1 to about 0.5, about 0.1 to about 0.4, or 0.15 to 0.35 dL/g. In one example, a feed is introduced to a feed inlet of the reactor to form the reaction medium and the It.V. of the feed is in the range of from about 0.1 to about 0.5, about 0.1 to about 0.4, or 0.15 to 0.35 dL/g.
  • [0046]
    The Intrinsic viscosity (It.V.) values are set forth in dL/g units as calculated from the inherent viscosity measured at 25° C. in 60% phenol and 40% 1,1,2,2-tetrachloroethane by weight. Polymer samples can be dissolved in the solvent at a concentration of 0.25 g/50 mL. The viscosity of the polymer solutions can be determined, for example, using a Rheotek Glass Capillary viscometer. A description of the operating principle of this viscometer can be found in ASTM D 4603. The inherent viscosity is calculated from the measured solution viscosity. The following equations describe such solution viscosity measurements and subsequent calculations to Ih.V. and from Ih.V. to It.V:
  • [0000]

    ηinh=[ln(t s /t o)]/C
  • [0047]
    where
      • ηinh=Inherent viscosity at 25° C. at a polymer concentration of 0.5 g/100 mL of 60% phenol and 40% 1,1,2,2-tetrachloroethane by weight
      • ln=Natural logarithm
      • ts=Sample flow time through a capillary tube
      • to=Solvent-blank flow time through a capillary tube
      • C=Concentration of polymer in grams per 100 mL of solvent (0.50%)
  • [0053]
    The intrinsic viscosity is the limiting value at infinite dilution of the specific viscosity of a polymer. It is defined by the following equation:
  • [0000]
    η int = lim C 0 ( η sp / C ) = lim C 0 ( ln η r ) / C
  • [0054]
    where
      • ηint=Intrinsic viscosity
      • ηr=Relative viscosity=ts/to
      • ηsp=Specific viscosity=ηr−1
        The intrinsic viscosity (It.V. or ηint) may be estimated using the Billmeyer equation as follows:
  • [0000]

    ηint=0.5[e 0.5×Ih.V.−1]+(0.75×Ih.V.)
  • [0000]
    The reference for estimating intrinsic viscosity (Billmeyer relationship) is J. Polymer Sci., 4, pp. 83-86 (1949).
  • [0058]
    The viscosity of the polymer solutions can also be determined using a Viscotek Modified Differential Viscometer (a description of the operating principle of the differential pressure viscometers can be found in ASTM D 5225) or other methods known to one skilled in the art.
  • [0059]
    In another embodiment of the present invention, there is provided a process for making polyethylene terephthalate (PET), the process comprising: (a) introducing a polycondensation feed into a polycondensation reactor, wherein the polycondensation feed forms a predominately liquid reaction medium in the reactor, wherein the polycondensation feed comprises PET having an average chain length in the range of from about 5 to about 100, about 5 to about 50, about 8 to about 40, or 10 to 30; (b) subjecting the reaction medium to polycondensation in the reactor, wherein the reactor comprises a substantially straight downwardly sloped pipe and at least 4, at least 6, or in the range of from about 2 to about 50, about 4 to about 25, or 6 to 15 spaced apart trays disposed at different elevations in the pipe, wherein the pipe is sloped downwardly at an angle in the range of from about 5 to about 75 degrees below horizontal, about 10 to about 60 degrees below horizontal, or 15 to 45 degrees below horizontal, wherein the reaction medium flows primarily by gravity through the reactor, wherein each of the trays presents an upwardly facing surface across which at least a portion of the reaction medium flows as the reaction medium flows through the reactor, wherein the upwardly facing surface is sloped less than about 10 degrees from horizontal, about 5 degrees from horizontal, or 2 degrees from horizontal, wherein each of the trays defines a plurality of apertures through which at least a portion of the reaction medium passes as the reaction medium flows through the reactor; and (c) recovering a predominately liquid polycondensation product from the reactor, wherein the polycondensation product comprises PET having an average chain length that is at least about 10, at least about 25, or at least 50 greater than the average chain length of the PET in the polycondensation feed. The detailed description of FIGS. 1 and 2, such as the tubular member, trays, and reaction medium flow, apply to this embodiment
  • [0060]
    In one example, the It.V. of the polycondensation feed is in the range of from about 0.1 to about 0.5, about 0.1 to about 0.4, or about 0.15 to about 0.35 dL/g. In one example, the It.V. of or polycondensation product is in the range of from about 0.3 to about 1.2, about 0.35 to about 0.6, or 0.4 to 0.5 dL/g.
  • [0061]
    In still another embodiment of the present invention, there is provided a reactor comprising a downwardly sloped tubular member and a plurality of spaced apart trays disposed at different elevations in the tubular member. The tubular member is elongated along a central axis of elongation that is oriented at a downward angle in the range of from about 5 to about 75 degrees below horizontal, about 10 to about 60 degrees below horizontal, or 15 to 45 degrees below horizontal. Each of the trays presents an upwardly facing surface that is sloped less than about 10 degrees from horizontal, about 5 degrees from horizontal, or 2 degrees from horizontal. The detailed description of FIGS. 1 and 2, such as the tubular member, trays, and reaction medium flow, apply to this embodiment
  • Numerical Ranges
  • [0062]
    The present description uses numerical ranges to quantify certain parameters relating to the invention. It should be understood that when numerical ranges are provided, such ranges are to be construed as providing literal support for claim limitations that only recite the lower value of the range, as well as claim limitations that only recite the upper value of the range. For example, a disclosed numerical range of 10 to 100 provides literal support for a claim reciting “greater than 10” (with no upper bounds) and a claim reciting “less than 100” (with no lower bounds).
  • Definitions
  • [0063]
    As used herein, the terms “a,” “an,” “the,” and “said” means one or more.
  • [0064]
    As used herein, the term “agitation” refers to work dissipated into a reaction medium causing fluid flow and/or mixing.
  • [0065]
    As used herein, the term “and/or,” when used in a list of two or more items, means that any one of the listed items can be employed by itself, or any combination of two or more of the listed items can be employed. For example, if a composition is described as containing components A, B, and/or C, the composition can contain A alone; B alone; C alone; A and B in combination; A and C in combination; B and C in combination; or A, B, and C in combination.
  • [0066]
    As used herein, the term “average chain length” means the average number of repeating units in the polymer. For a polyester, average chain length means the number of repeating acid and alcohol units. Average chain length is synonymous with the number average degree of polymerization (DP). The average chain length can be determined by various means known to those skilled in the art. For example, 1H-NMR can be used to directly determine the chain length based upon end group analysis, and light scattering can be used to measure the weight average molecular weight with correlations used to determine the chain length. Chain length is often calculated based upon correlations with gel permeation chromotagraphy (GPC) measurements and/or viscosity measurements.
  • [0067]
    As used herein, the terms “comprising,” “comprises,” and “comprise” are open-ended transition terms used to transition from a subject recited before the term to one or more elements recited after the term, where the element or elements listed after the transition term are not necessarily the only elements that make up the subject.
  • [0068]
    As used herein, the terms “containing,” “contains,” and “contain” have the same open-ended meaning as “comprising,” “comprises,” and “comprise,” provided below.
  • [0069]
    As used herein, the term “conversion” is used to describe a property of the liquid phase of a stream that has been subjected to esterification, wherein the conversion of the esterified stream indicates the percentage of the original acid end groups that have been converted (i.e., esterified) to ester groups. Conversion can be quantified as the number of converted end groups (i.e., alcohol end groups) divided by the total number of end groups (i.e., alcohol plus acid end groups), expressed as a percentage.
  • [0070]
    As used herein, the term “directly coupled” refers to a manner of coupling two vessels in fluid flow communication with one another without the use of an intermediate connector having a substantially narrower diameter than the two vessels.
  • [0071]
    As used herein, the term “esterification” refers to both esterification and ester exchange reactions.
  • [0072]
    As used herein, the terms “having,” “has,” and “have” have the same open-ended meaning as “comprising,” “comprises,” and “comprise,” provided above.
  • [0073]
    As used herein, the terms “including,” “includes,” and “include” have the same open-ended meaning as “comprising,” “comprises,” and “comprise,” provided above.
  • [0074]
    As used herein, the term, “mechanical agitation” refers to agitation of a reaction medium caused by physical movement of a rigid or flexible element(s) against or within the reaction medium.
  • [0075]
    As used herein, the term “open flow area” refers to the open area available for fluid flow, where the open area is measured along a plane that is perpendicular to the direction of flow through the opening.
  • [0076]
    As used herein, the term “percent open” refers to the area of a structure that is open for fluid flow therethrough as a percentage of the total area of the structure measured normal to the direction of flow though the openings in the structure.
  • [0077]
    As used herein, the term “pipe” refers to a substantially straight elongated tubular member having a generally cylindrical sidewall.
  • [0078]
    As used herein, the terms “polyethylene terephthalate” and “PET” include PET homopolymers and PET copolymers.
  • [0079]
    As used herein, the terms “polyethylene terephthalate copolymer” and “PET copolymer” mean PET that has been modified by up to 10 mole percent with one or more added comonomers. For example, the terms “polyethylene terephthalate copolymer” and “PET copolymer” include PET modified with up to 10 mole percent isophthalic acid on a 100 mole percent carboxylic acid basis. In another example, the terms “polyethylene terephthalate copolymer” and “PET copolymer” include PET modified with up to 10 mole percent 1,4-cyclohexane dimethanol (CHDM) on a 100 mole percent diol basis.
  • [0080]
    As used herein, the term “polyester” refers not only to traditional polyesters, but also includes polyester derivatives, such as, for example, polyetheresters, polyester amides, and polyetherester amides.
  • [0081]
    As used herein, “predominately liquid” means more than 50 volume percent liquid.
  • [0082]
    As used herein, the term “reaction medium” refers to any medium subjected to chemical reaction.
  • [0083]
    As used herein, the term “residue” refers to the moiety that is the resulting product of the chemical species in a particular reaction scheme or subsequent formulation or chemical product, regardless of whether the moiety is actually obtained from the chemical species.
  • [0084]
    As used herein, the term “vapor byproduct” includes the vapor generated by a desired chemical reaction (i.e., a vapor coproduct) and any vapor generated by other reactions (i.e., side reactions) of the reaction medium.
  • CLAIMS NOT LIMITED TO DISCLOSED EMBODIMENTS
  • [0085]
    The exemplary embodiments of the invention described above are to be used as illustration only, and should not be used in a limiting sense to interpret the scope of the claimed invention. Various modifications to the above-described exemplary embodiments could be readily made by those skilled in the art without departing from the scope of the invention as set forth in the following claims.
Citas de patentes
Patente citada Fecha de presentación Fecha de publicación Solicitante Título
US2709642 *3 Dic 195131 May 1955Exxon Research Engineering CoChemical reactor
US2820815 *8 Abr 195421 Ene 1958Exxon Research Engineering CoSynthetic lubricating compositions and process for their preparation
US2829153 *4 Mar 19571 Abr 1958Du PontContinuous ester interchange process
US2973341 *28 Ene 195728 Feb 1961Glanzstoff AgContinuous process for production of a polyethylene terephthalate condensate
US3185668 *31 Ago 195925 May 1965Standard Oil CoDirect esterification
US3192184 *19 Mar 195929 Jun 1965Du PontPrepolymerization process
US3241926 *15 Nov 196322 Mar 1966Monsanto CoApparatus for continuously polycondensing polymethylene glycol esters of aromatic dicarboxylic acids
US3250747 *7 Dic 196110 May 1966Eastman Kodak CoPolyesterification in two evacuated zones separated by a liquid seal
US3251657 *9 May 196317 May 1966Hoechst AgReactor for the manufacture of polyethylene phthalates
US3254965 *4 Dic 19647 Jun 1966Phillips Petroleum CoPolymerization control apparatus
US3376353 *17 Mar 19672 Abr 1968Monsanto CoRecovery of glycols from polyester production
US3385881 *20 Jun 196328 May 1968Hoechst AgProcess for the continuous preparation of monomeric and oligomeric bis-2-hydroxyethyl phthalates
US3427287 *30 Jun 196611 Feb 1969Goodyear Tire & RubberMethod for preparing polyester resins
US3438942 *1 Jun 196515 Abr 1969Vickers Zimmer AgContinuous polyester process
US3442868 *15 Jul 19666 May 1969Teijin LtdNovel process for the preparation of polyester
US3496146 *23 Ago 196717 Feb 1970Du PontPreparation of glycol terephthalate linear polyester by direct esterification of terephthalic acid
US3496159 *27 Mar 196717 Feb 1970Spence & Green Chem CoEsterification of fatty acids of tall oil in a horizontal distillation column and condenser
US3496220 *28 Oct 196617 Feb 1970Mobil Oil CorpEsterification process
US3497473 *29 Nov 196624 Feb 1970American Enka CorpProcess for the preparation of polyethylene terephthalate
US3507905 *3 Jun 196621 Abr 1970Rhone Poulenc SaContinuous preparation of glycol phthalates
US3509203 *16 Dic 196628 Abr 1970Engels Chemiefaserwerk VebTransesterification of dicarboxylic alkyl esters with glycols
US3582244 *8 Dic 19691 Jun 1971Snia ViscosaDevice for volumetrically removing viscous liquids from vacuum operating equipments
US3590070 *3 Jun 196829 Jun 1971Celanese CorpRecycle of terephthalic acid in the production of a bis(2-hydroxyalkyl) terephthalate
US3590072 *18 Nov 196629 Jun 1971Monsanto CoMethod for direct esterification of terephthalic acid with ethylene glycol
US3639448 *21 Dic 19671 Feb 1972Mitsubishi Chem IndProcess for producing bis(beta-hydroxyethyl)-terephthalate and/or prepolymer thereof
US3644096 *30 Mar 197022 Feb 1972Eastman Kodak CoApparatus for use in a continuous flow reaction for producing a monomer and/or a protopolymer
US3644294 *4 Abr 196922 Feb 1972Snia ViscosaProcess and equipment for the continuous production of polyesters
US3644483 *12 Sep 196722 Feb 1972Inventa AgContinuous manufacture of fiber-forming polyesters
US3646102 *11 Ago 196929 Feb 1972Idemitsu Kosan CoMethod for continuously preparing polycarbonate oligomer
US3647758 *22 Ene 19707 Mar 1972Inventa AgProcess and apparatus for the continuous production of polyamides and polyesters
US3651125 *12 Ago 196821 Mar 1972Eastman Kodak CoContinuous method for formation of a liquid monomer for a condensation polymer
US3723391 *18 Nov 197027 Mar 1973Basf AgContinuous manufacture of polyesters
US3740267 *22 Sep 197119 Jun 1973Allied ChemMethod of cleaning apparatus used in processing polyethylene terephthalate
US3787479 *20 May 197022 Ene 1974Inventa AgProcess for the continuous transesterification of dicarboxylic acid alkyl esters with diols
US3819585 *26 Ene 197325 Jun 1974Monsanto CoPolyester esterification under two different pressures
US3867349 *3 May 197318 Feb 1975Davy Ashmore AgAddition of dimethyl terephthalate and ethylene glycol to recycled bis(hydroxyethyl)terephthalate
US3960820 *8 Nov 19741 Jun 1976Du Pont Of Canada LimitedRegulating the flow of molten polyamides in a continuous process for the preparation thereof
US4001187 *11 Jul 19744 Ene 1977Kanebo, Ltd.Method of producing polyesters terephthalic acid and ethylene glycol
US4008048 *3 Jul 197415 Feb 1977Agfa-Gevaert N.V.Installation for the discontinuous production of polyethylene terephthalate
US4019866 *10 Ene 197526 Abr 1977Du Pont Of Canada LimitedRecirculating reaction apparatus for continuous preparation of a polyamide
US4020049 *2 Abr 197126 Abr 1977The Goodyear Tire & Rubber CompanyProcess for preparing polyester resin
US4077945 *18 Abr 19777 Mar 1978Zimmer AktiengesellschaftProcess for making linear polyesters from ethylene glycol and terephthalic acid
US4079046 *3 Jun 197614 Mar 1978Monsanto Company, St. Louis, MissouriMultiple polyesterification process
US4089888 *12 Jul 197616 May 1978Idemitsu Petrochemical Co. Ltd.Method for producing a polycarbonate oligomer
US4146729 *7 Abr 197727 Mar 1979E. I. Du Pont De Nemours And CompanyProcess for preparing poly(ethylene terephthalate)
US4148693 *17 Feb 197710 Abr 1979Williamson William RHorizontal cylindrical distillation apparatus
US4196168 *5 May 19781 Abr 1980Eastman Kodak CompanySloped tray arrangement for polymerization reactor
US4200145 *12 Ene 197829 Abr 1980The Badger Company, Inc.Method of preheating a liquid reaction mass of polyolefin dissolved in liquid monomer
US4204070 *23 Abr 197620 May 1980Fuji Photo Film Co., Ltd.Process for preparing polyethylene terephthalate and its low molecular weight oligomers
US4254246 *26 Mar 19793 Mar 1981Davy International AgColumn system process for polyester plants
US4382139 *10 Dic 19813 May 1983Didier Engineering GmbhProcess and apparatus for continuous production of polyesters
US4383093 *3 Jun 198110 May 1983Mitsui Petrochemical Industries Ltd.Tubular polymerization reactor, and process for polymerization
US4424301 *30 Jul 19813 Ene 1984Hoechst AktiengesellschaftContinuous process and device for the manufacture of a vinyl chloride polymer in aqueous suspension
US4440924 *15 Sep 19833 Abr 1984Toyo Boseki Kabushiki KaishaProcess for production of polyester
US4499226 *30 Dic 198212 Feb 1985The Goodyear Tire & Rubber CompanyHigh clarity colorless polyesters
US4588560 *29 Jun 198413 May 1986Mobil Oil CorporationHydroprocessing reactor for catalytically dewaxing liquid petroleum feedstocks
US4721575 *3 Abr 198626 Ene 1988Vertech Treatment Systems, Inc.Method and apparatus for controlled chemical reactions
US5002116 *30 Jul 199026 Mar 1991Airxchange, Inc.Rotary heat regenerator
US5185426 *20 Feb 19929 Feb 1993Agfa-Gevaert, N.V.Process for the production of polyester with enhanced thermo-oxidative stability
US5194525 *6 Ago 199116 Mar 1993Dainippon Ink And Chemicals, Inc.Continuous mass polymerization process for making styrene copolymers
US5202463 *10 Sep 199113 Abr 1993Arco Chemical Technology, L.P.Process for the preparation of a glycol ether ester
US5294305 *6 May 199315 Mar 1994Mobile Process Technology, Inc.Ethylene glycol recovery process
US5300626 *3 Abr 19915 Abr 1994Rhone-Poulenc FibresProcess for obtaining modified polyethylene terephthalate pilling-free fibres originating from the polymer thus modified
US5384389 *19 Nov 199324 Ene 1995Bayer AktiengesellschaftProcess for the production of polycarbonates
US5385773 *27 Abr 199331 Ene 1995Eastman Chemical CompanyCopolyester of cyclohexanenedimethanol and process for producing such polyester
US5413861 *3 Feb 19949 May 1995Dextor CorporationSemiconductor device encapsulated with a flame retardant epoxy molding compound
US5480616 *26 Jul 19942 Ene 1996Amoco CorporationPolycondensation apparatus
US5484882 *8 Jul 199416 Ene 1996Dainippon Ink And Chemicals, Inc.Process for the continuous production of biodegradable polyester polymer
US5496469 *28 Dic 19945 Mar 1996Scraggs; Charles R.Apparatus for reducing and separating emulsions and homgeneous components from contaminated water
US5519112 *21 Dic 199421 May 1996Mitsui Petrochemical Industries Ltd.Method of manufacturing polyesters
US5594077 *25 Oct 199414 Ene 1997Bayer AgProcess for preparing polymers which contain aspartic acid
US5599900 *16 Abr 19964 Feb 1997E. I. Du Pont De Nemours And CompanyPolyesters production process
US5602216 *22 Jul 199611 Feb 1997Sulzer Chemtech AgProcess and apparatus for performing a polymerisation in a tube reactor
US5739219 *1 Jul 199614 Abr 1998Basf AktiengesellschaftContinuous preparation of polymers
US5750079 *27 Nov 199612 May 1998Shin-Etsu Chemical Co., Ltd.Polymerization apparatus of producing vinyl chloride type polymer
US5753190 *21 Jul 199519 May 1998Eastman Chemical CompanyVacuum system for controlling pressure in a polyester process
US5753784 *1 Jul 199619 May 1998Basf AktiengesellschaftContinuous preparation of polymers and apparatus for this purpose
US5898058 *20 May 199627 Abr 1999Wellman, Inc.Method of post-polymerization stabilization of high activity catalysts in continuous polyethylene terephthalate production
US5902865 *6 May 199711 May 1999Basf AktiengesellschaftPreparation of polystyrene by continuous anionic polymerization
US5905096 *19 Ago 199618 May 1999Basf AktiengesellschaftContinuous production process of expandable styrene polymer beads
US6069228 *17 Ago 199830 May 2000E. I. Du Pont De Nemours And CompanyProcess for preparing polyamides
US6174970 *4 Mar 199716 Ene 2001Basf AktiengesellschaftMethod of reprocessing residues containing dihydroxy compounds
US6339031 *29 Dic 199815 Ene 2002Seng C. TanMicrocellular carbon foams and microcellular C/C composites fabricated therefrom
US6355738 *26 Feb 199912 Mar 2002Mitsui Chemicals IncPolyester and process for preparing polyester
US6359106 *22 Ago 200019 Mar 2002Hitachi, Ltd.Production process and production apparatus for polybutylene terephthalate
US6545176 *28 Oct 19998 Abr 2003Rohm And Haas CompanyApparatus and process for the high yield production of methyl methacrylate or methacrylic acid
US6551517 *9 Jul 199922 Abr 2003L'electrolyseMethod for transforming chemical structures in a fluid under pressure and in high temperature
US6703454 *7 Dic 20019 Mar 2004Eastman Chemical CompanyAdsorber system to replace water column in a polyester process
US6723826 *28 May 200320 Abr 2004Hitachi, Ltd.Production process and production apparatus for polybutylene terephthalate
US6861494 *7 Dic 20011 Mar 2005Eastman Chemical CompanyPolyester process using a pipe reactor
US7008546 *7 Ene 20037 Mar 2006Jerry M EdmondsonOil, water and gas separator for swaying service
US7049462 *27 Nov 200123 May 2006Nippon Shokubai Co., Ltd.Production process for product of dehydration reaction and apparatus used for the production
US20030019126 *29 Jul 200230 Ene 2003Martin GreiveDrying station and method for drying printed sheets and printing machine having a drying station
US20030037910 *26 Ago 200227 Feb 2003Genrikh SmyrnovMethod of action of the pulsating heat pipe, its construction and the devices on its base
US20040068070 *29 May 20038 Abr 2004Basf AktiengesellcschaftPreparation of readily polymerizable compounds
US20050059782 *13 Oct 200417 Mar 2005Andrist Kevin M.Continuous bulk polymerization and esterification process and compositions
US20060008661 *29 Jul 200412 Ene 2006Wijesundara Muthu BManufacturable low-temperature silicon carbide deposition technology
US20070065211 *6 Mar 200622 Mar 2007Toshiba Tec Kabushiki KaishaDot head and method of manufacturing armature structure for dot head
US20090016940 *12 Jul 200715 Ene 2009Eastman Chemical CompanySloped tubular reactor with divided flow
Citada por
Patente citante Fecha de presentación Fecha de publicación Solicitante Título
US7842777 *12 Jul 200730 Nov 2010Eastman Chemical CompanySloped tubular reactor with divided flow
US79430947 Dic 200617 May 2011Grupo Petrotemex, S.A. De C.V.Polyester production system employing horizontally elongated esterification vessel
US84702504 Abr 201125 Jun 2013Grupo Petrotemex, S.A. De C.V.Polyester production system employing horizontally elongated esterification vessel
US20080139760 *7 Dic 200612 Jun 2008Debruin Bruce RogerPolyester production system employing horizontally elongated esterification vessel
US20090016940 *12 Jul 200715 Ene 2009Eastman Chemical CompanySloped tubular reactor with divided flow
US20110184130 *4 Abr 201128 Jul 2011Grupo Petrotemex, S.A. De C.V.Polyester production system employing horizontally elongated esterification vessel
Clasificaciones
Clasificación de EE.UU.422/131, 526/64
Clasificación internacionalC08F2/01
Clasificación cooperativaB01J19/006, B01J2219/0077, B01J2219/1943, C08G63/785, B01J2219/187, B01J19/2415, C08G63/183, B01J2219/00777
Clasificación europeaB01J19/00D2, B01J19/24D, C08G63/78A
Eventos legales
FechaCódigoEventoDescripción
9 Ago 2007ASAssignment
Owner name: EASTMAN CHEMICAL COMPANY, TENNESSEE
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:WINDES, LARRY CATES;DEBRUIN, BRUCE ROGER;EKART, MICHAEL PAUL;REEL/FRAME:019671/0954;SIGNING DATES FROM 20070710 TO 20070711
Owner name: EASTMAN CHEMICAL COMPANY, TENNESSEE
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:WINDES, LARRY CATES;DEBRUIN, BRUCE ROGER;EKART, MICHAEL PAUL;SIGNING DATES FROM 20070710 TO 20070711;REEL/FRAME:019671/0954
1 Feb 2011ASAssignment
Owner name: GRUPO PETROTEMEX, S.A. DE C.V., MEXICO
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:EASTMAN CHEMICAL COMPANY;REEL/FRAME:025727/0271
Effective date: 20110131
11 Jun 2014FPAYFee payment
Year of fee payment: 4